Apparatus for producing carbonic acid diester

ABSTRACT

A process for producing a carbonic acid diester, which comprises carrying out a reaction in a vapor phase of an alcohol, carbon monoxide and oxygen in the presence of a catalyst in a fluidized-bed reactor so that an oxidative carbonylation of the alcohol occurs, thereby obtaining a carbonic acid diester, wherein a heat of reaction is removed by the latent heat of vaporization of the alcohol as a raw material. In the process, for example, either at least part of the alcohol may be directly fed in liquid phase into the fluidized bed or cooling pipes are disposed in the fluidized bed and at least part of the alcohol is introduced in liquid phase into the cooling pipes as a heat transfer medium so that the liquid alcohol is vaporized and fed into the fluidized-bed reactor. Carbon monoxide may be introduced together with the liquid alcohol into the cooling pipes. A process of high energy efficiency realizing an effective utilization of a heat of reaction and an apparatus therefor are provided in the production of a carbonic acid diester in a vapor phase with the use of a fluidized-bed reactor.

This application is a divisional of U.S. Pat. application Ser. No.08/896,228, filed Jul. 17, 1997, now U.S. Pat. No. 5,831,113, issuedNov. 3, 1998.

FIELD OF THE INVENTION

The present invention relates to a process for producing a carbonic aciddiester, in which the carbonic acid diester is produced in a vapor phasewith the use of a fluidized-bed reactor, and an apparatus therefor.

BACKGROUND OF THE INVENTION

Carbonic acid diester such as dimethyl carbonate are attractingattention as a raw material substituted for phosgene or dimethyl sulfatein the production of isocyanates, polycarbonates and various drugs andagricultural chemicals. Further, the use thereof as an additive toautomobile fuel is being considered.

Carbonic acid diester has long been produced by reacting phosgene withan alcohol. However, the use of phosgene has drawbacks in that phosgeneis highly toxic and that the reaction forms hydrochloric acid as aby-product, which causes corrosion of the apparatus. Therefore,processes for producing the carbonic acid diester without the use ofphosgene have been developed and are now being executed on industrialscales.

For example, Japanese Patent Laid-open Publication No. 54(1979)-24827discloses a process for producing a carbonic acid diester, in which analcohol, carbon monoxide and oxygen react in the liquid phase in thepresence of a copper halide catalyst. Furthermore, Japanese PatentLaid-open Publication No. 50(1975)-40528, Japanese Patent PublicationNo. 61(1986)-8816 and Japanese Patent Laid-open Publication Nos.62(1987)-81356 and 1(1989)-287062 disclose processes for producing thecarbonic acid diester in liquid phase, in which copper and palladiumhalides are used as catalytic components.

Although having the advantage of using no phosgene, the above processesfor producing a carbonic acid diester in the liquid phase have drawbacksin that (1) the reaction apparatus is likely to corrode by the action ofa halide catalyst which is used as a solution (2), the catalyst activityis deteriorated rapidly by the water formed during the reaction and (3)it is difficult to separate the catalyst dissolved in the reactionproduct. In particular, it is requisite that the reaction apparatus isconstructed of a corrosion resistant high-quality material to therebyprevent the corrosion of the apparatus and any disaster attributed tothe corrosion. This inevitably causes the construction cost of theapparatus to be extremely high.

Processes for producing carbonic acid diester by vapor phase reactionhave been proposed as substitutes for the liquid phase processes (forexample, Published Japanese Translation of PCT Patent Applications fromOther States, No. 63(1988)-503460, Japanese Patent Laid-open PublicationNo. 4(1992)-89458 and International Application Publication WO90/15791).

In the vapor phase processes disclosed in these publications, vaporizedalcohol, carbon monoxide and oxygen react in the vapor phase in thepresence of a catalyst, and the resultant gaseous reaction product iswithdrawn from the reactor. The withdrawn gas is cooled to therebyseparate it into a condensed liquid and a noncondensable gas and thecarbonic acid diester is separated from the liquid. These vapor phaseprocesses are substantially free from the above drawbacks of the liquidphase processes.

Apart from the above, the oxidative carbonylation of an alcohol is anexothermic reaction. The heat of reaction must be removed formaintaining an appropriate reaction temperature. For example, thecalorific values are about 71 kcal/mol in both of the followingreactions in which carbonic acid diesters are prepared from methanol andethanol:

    2CH.sub.3 OH+CO+1/2O.sub.2 →(CH.sub.3 O).sub.2 CO+H.sub.2 O, and

    2C.sub.2 H.sub.5 OH+CO+1/2O.sub.2 →(C.sub.2 H.sub.5 O).sub.2 CO+H.sub.2 O.

When a catalyst consists of, for example, a copper oxychloride supportedon an active carbon, the above oxidative carbonylation of an alcohol inthe vapor phase is conducted at a temperature as relatively low as about130 to 170° C.

When it is attempted to synthesize a carbonic acid diester by the use ofa fixed-bed reactor, hot spots are likely to occur because the reactionis highly exothermic, so that the dangers of decrease of reactionselectivity, runaway of reaction and catalyst deactivation areincreased.

By contrast, the heat of reaction can be removed much more easily in afluidized-bed reactor than in the fixed-bed reactor, so that thetemperature can be controlled without the occurrence of hot spots.

In the above vapor phase reaction in the fluidized-bed reactor,generally, cooling pipes are inserted in the fluidized bed so as toeffect heat removal and water is generally used as the heat transfermedium. For example, International Application Publication WO 95/21692discloses a fluidized-bed reactor for vapor-phase exothermic reactionwhich is provided with cooling pipes capable of feeding a cooling mediumat a steady rate and cooling pipes capable of feeding a cooling mediumat a variable rate. In the publication, water is mentioned as thecooling medium fed at a steady rate and steam is mentioned as thecooling medium fed at a variable rate.

If steam obtained by the vaporization resulting from the removal of theheat of reaction generated in the fluidized bed can be used as, forexample, a heat source for a reboiler of a distillation column,effective utilization of the heat of reaction would be attained. Whenthe difference between the reaction temperature and the temperature ofthe heat transfer medium flowing through the cooling pipes is large, theremoval of the heat of reaction would be easy.

In the oxidative carbonylation conducted at relatively low temperatures,the difference between the reaction temperature and the temperature ofsteam available as a heat source (for example, about 125° C. withrespect to reboiler heat source) is so small that the number of coolingpipes must be increased to thereby enlarge the heat-transfer area inorder to obtain the steam of the above temperature.

However, the number of cooling pipes which can be inserted in afluidized bed of a given volume is so limited that it is likely that theheat-transfer area required for the removal of heat cannot besatisfactorily secured. Further, when the removal of heat is attemptedby increasing the difference between the reaction temperature and thetemperature of heat transfer medium under the condition of the limitednumber of cooling pipes, only low-temperature steam or water can beobtained which has little value.

On the other hand, the attempt to increase the heat-transfer area leadsto an unnecessary expansion of the volume of the fluidized bed.

Therefore, there has been a demand for the development of a processcapable of producing a carbonic acid diester in high energy efficiencywith the effective utilization of the heat of reaction in thevapor-phase oxidative carbonylation of an alcohol which is conducted atrelatively low temperatures.

OBJECT OF THE INVENTION

The present invention has been made taking the above prior art intoaccount. An object of the present invention is to provide a vapor-phaseprocess for producing a carbonic acid diester by means of afluidized-bed reactor wherein the carbonic acid diester can be producedin high energy efficiency with the effective utilization of the heat ofreaction, and another object of the present invention is to provide anapparatus for producing a carbonic acid diester which is suitable forthe above process.

SUMMARY OF THE INVENTION

The process for producing a carbonic acid diester according to thepresent invention comprises carrying out a reaction in a vapor phase ofan alcohol, carbon monoxide and oxygen in the presence of a catalyst ina fluidized-bed reactor so that an oxidative carbonylation of thealcohol occurs, thereby obtaining a carbonic acid diester, wherein aheat of reaction is removed by the latent heat of vaporization of thealcohol used as a raw material.

In a particular mode of the process, at least part of the alcohol as araw material is fed in liquid phase into a fluidized bed of the reactor.

In another mode of the process, cooling pipes are provided in afluidized bed of the reactor and at least part of the alcohol as a rawmaterial is introduced in liquid phase into the cooling pipes as a heattransfer medium so that at least part of the liquid alcohol is vaporizedand fed into the fluidized-bed reactor. In this mode of the process,carbon monoxide can be introduced together with the liquid alcohol intothe cooling pipes.

In the above modes of the process, cooling pipes in which water or anoil is introduced as a heat transfer medium can be provided in afluidized bed of the reactor.

In the present invention, the process can be conducted in such a modethat cooling pipes are provided in a fluidized bed of the reactor andthe alcohol as a raw material is introduced in liquid phase thereinto asa heat transfer medium so that the liquid alcohol is heated to anincreased temperature,

the heated liquid alcohol is fed into an evaporator in which the liquidalcohol is mixed with carbon monoxide and at least part of the alcoholis vaporized, and

the vaporized alcohol is fed together with the carbon monoxide into thefluidized-bed reactor.

In the present invention, moreover, the process can be conducted in sucha mode that cooling pipes are provided in a fluidized bed of the reactorand water or an oil as a heat transfer medium is circulatedtherethrough, the obtained hot water or hot oil being passed through aheat exchanger to thereby effect a heat exchange between the hot wateror oil and a liquid alcohol so that the liquid alcohol is heated to havean increased temperature, the heated liquid alcohol is fed into anevaporator in which the liquid alcohol is mixed with carbon monoxide andat least part of the alcohol is vaporized, and

the vaporized alcohol is fed together with the carbon monoxide into thefluidized-bed reactor.

The apparatus for producing a carbonic acid diester according to thepresent invention comprises:

a fluidized-bed reactor 1 adapted to carry out a reaction in a vaporphase of an alcohol, carbon monoxide and oxygen in the presence of acatalyst so that an oxidative carbonylation of the alcohol occurs tothereby form a carbonic acid diester,

an evaporator 12 adapted to mix a liquid alcohol with carbon monoxideand vaporize at least part of the alcohol to thereby form a gaseousmixture of alcohol and carbon monoxide and adapted to feed the gaseousmixture through a gas supply line 3 into the fluidized-bed reactor 1,

cooling pipes 7 arranged in the fluidized-bed reactor 1 and adapted tocause a liquid alcohol 9 as a heat transfer medium 8 capable of removinga heat of reaction generated by the oxidative carbonylation of thealcohol in the fluidized-bed reactor 1 to flow therethrough, and

a heated alcohol supply line 14 adapted to feed the liquid alcohol 9heated in the fluidized-bed reactor 1 from the cooling pipes 7 into theevaporator 12.

Furthermore, the apparatus for producing a carbonic acid diesteraccording to the present invention may comprise:

the fluidized-bed reactor 1,

the evaporator 12,

cooling pipes 7 arranged in the fluidized-bed reactor 1 and adapted tocause a heat transfer medium 8 capable of removing a heat of reactiongenerated by the oxidative carbonylation of the alcohol in thefluidized-bed reactor 1 to flow therethrough,

a heat transfer medium withdrawal line 17 adapted to lead the heattransfer medium 8 heated in the fluidized-bed reactor 1 from the coolingpipes 7 to a heat exchanger 19,

the heat exchanger 19 adapted to conduct a heat exchange between theheat transfer medium 8 and a liquid alcohol 9 so that the liquid alcohol9 is heated to an increased temperature, and

a heated alcohol supply line 12g adapted to feed the liquid alcohol 9heated by the heat exchanger 19 into the evaporator 12.

BRIEF DESCRIPTION OF THE DRAWING

FIG. 1 schematically shows one mode of the process for producing acarbonic acid diester according to the present invention;

FIG. 2 shows another mode of the process for producing a carbonic aciddiester according to the present invention;

FIG. 3 shows a further other mode of the process for producing acarbonic acid diester according to the present invention;

FIG. 4 shows one form of the apparatus for producing a carbonic aciddiester according to the present invention; and

FIG. 5 shows another form of the apparatus for producing a carbonic aciddiester according to the present invention.

DETAILED DESCRIPTION OF THE INVENTION

The process for producing a carbonic acid diester and the apparatus forproducing a carbonic acid diester according to the present inventionwill be described in detail below.

Process for oroducina carbonic acid diester

The present invention provides a process for producing a carbonic aciddiester, which comprises carrying out a reaction in a vapor phase of analcohol, carbon monoxide and oxygen in the presence of a catalyst in afluidized-bed reactor so that an oxidative carbonylation of the alcoholoccurs, thereby obtaining a carbonic acid diester, wherein a heat ofreaction is removed by the latent heat of vaporization of the alcoholused as a raw material. In particular, at least part of a liquid alcoholas a raw material of the carbonylation is vaporized by the heat ofreaction and, simultaneously, the heat of reaction is removed by thelatent heat of vaporization of the alcohol, and the vaporized alcohol issubjected to the carbonylation.

For example, in one mode of the process, at least part of an alcohol asa raw material of the carbonylation is directly fed in liquid phase intothe fluidized bed.

This process is schematically shown in FIG. 1.

Referring to FIG. 1, a fluidizing gas is introduced into a fluidized-bedreactor 1 charged with a solid catalyst through a gas supply line 3provided at a bottom of the fluidized-bed reactor 1 and is fed through agas distributor la provided in the reactor 1 so that the solid catalystforms a fluidized bed 4. An inert gas such as nitrogen can also be usedas an initial fluidizing gas to form the fluidized bed. Thecarbonylation is initiated by replacing the inert gas with a gas of araw material.

Carbon monoxide and oxygen are generally introduced through the gassupply line 3 and fed through the gas distributor 1a into the fluidizedbed 4 in order to perform the carbonylation in the vapor phase in thepresence of a catalyst. At least part of the alcohol as a raw materialis directly introduced in liquid phase into the fluidized bed 4 through,for example, a line 2.

Upon the feeding of the alcohol in liquid phase into the fluidized bed4, the alcohol is vaporized to thereby undergo the carbonylation in thevapor phase and, simultaneously, the heat of reaction is removed by thelatent heat of vaporization of the alcohol.

Simultaneously with the above liquid alcohol, vaporized alcohol can beintroduced into the fluidized bed 4 by feeding the alcohol vaporized inadvance through, for example, a line 3.

At least part of the alcohol may be introduced in liquid phase in theabove direct feeding of the liquid alcohol into the fluidized bed 4.Although the proportion of the alcohol fed in liquid phase variesdepending on the reaction conditions and the relationship in magnitudebetween the heat of reaction and the latent heat of vaporization, thisproportion can be calculated on the basis of the quantity which can bevaporized by the heat of reaction and generally ranges from about 20 to100%, preferably, from about 70 to 100% based on the total amount of thealcohol used in the carbonylation.

The feeding of the liquid alcohol is generally conducted at a pressurewhich is higher than the reaction pressure so that the liquid alcoholcan be fed into the fluidized bed and at a temperature at which thealcohol can maintain its liquid state at the feeding pressure.

The reaction product is generally withdrawn through a line 5 provided atthe top of the fluidized-bed reactor.

The oxygen introduced through the line 3 for the carbonylation may bepure molecular oxygen or may be one diluted with an inert gas such asnitrogen or argon.

The carbon monoxide introduced for the carbonylation is not limited topure carbon monoxide. A gas which contains carbon monoxide may be used.Examples of such gases include a gaseous mixture of carbon monoxide andother components which are inert in the reaction, such as nitrogen,methane, hydrogen or carbon dioxide.

Although the carbon monoxide concentration of such a gaseous mixture isnot particularly limited, it is generally preferred to be at least 70%from the economic point of view in the production of the carbonic aciddiester.

The product gas from the fluidized-bed reactor can be recycled as acarbon monoxide source.

In the execution of the recycling, for example, part of the product gasfrom the fluidized-bed reactor 1 can be cooled and introduced into avapor-liquid separator 6 by which the gas is separated from the liquid,and the separated gas can be compressed and recycled through a gasrecycle line 6 a to the fluidized-bed reactor 1, as shown in FIG. 1.

The gas separated by the vapor-liquid separator 6 may be introduced intoa CO₂ -removing device in which at least part of carbon dioxide formedas a by-product is removed by absorption or adsorption before thecirculation to the fluidized-bed reactor 1. Further, part of the recyclegas may be discharged from a branch pipe 6b so that the concentration ofimpurities such as carbon dioxide is controlled.

Carbon monoxide may be added to the recycle gas at an arbitrary point(not shown) of the recycle line 6a.

Herein, as apparent from the above, the "carbon monoxide source" is usedto mean not only pure carbon monoxide but also a gaseous mixture and aproduct gas which contain carbon monoxide collectively.

On the other hand, the liquid phase separated by the vapor-liquidseparator 6 is generally led to a purification step (not shown), inwhich the liquid is, for example, distilled to obtain the desiredcarbonic acid diester.

In the present invention, the removal of the heat of reaction from thefluidized bed may be accomplished only by the above latent heat ofvaporization of the alcohol. In addition to the latent heat ofvaporization of the alcohol, the removal of the heat of reaction may beperformed with the aid of cooling pipes 7 inserted in the fluidized bed4 as shown in FIG. 2. Water or an oil can be used as a heat transfermedium 8 for the cooling pipes 7. For example, water heated at 70 to100° C. may be used as the heat transfer medium.

Examples of suitable oils include commercially available heat transferfluids comprising as a principal component an aromatic hydrocarbon suchas diphenyl or terphenyl or an aromatic ether such as diphenyl ether andsilicone oils.

A required number of cooling pipes 7 are provided in the fluidized bed.Reference characters in FIG. 2 correspond to those in FIG. 1.

In the present invention, the heat of reaction can be removed by thelatent heat of vaporization of the alcohol as a raw material of thecarbonylation in another mode of the process as shown in FIG. 3.Reference characters in FIG. 3 correspond to those in FIG. 1.

Referring now to FIG. 3, at least part of an alcohol as a raw materialof the carbonylation is introduced in liquid phase as a heat transfermedium 9 in cooling pipes 7 arranged in a fluidized bed 4 and at leastpart of the liquid alcohol is vaporized and fed into the fluidized-bedreactor 1. The liquid alcohol introduced in the cooling pipes 7 isheated in the fluidized-bed 4, so that at least part thereof isvaporized and, simultaneously, the heat of reaction can be removed.

The above use of the alcohol as the heat transfer medium 9 passedthrough the cooling pipes 7 enables the alcohol to be heated tosubstantially the same temperature as the reaction temperature.Therefore, even if the reaction temperature is as low as about 130 to170° C., at least part, preferably, all of the alcohol heated to thereaction temperature can be obtained in vapor phase, so that the heat ofreaction can effectively be utilized.

The alcohol 9 vaporized in the cooling pipes 7 is introduced in anoptionally installed vapor-liquid separator 10 by which liquid alcoholis separated. The vaporized alcohol after the separation is recycledthrough, for example, a line 10a and a line 3 to the fluidized-bedreactor 1. After the separation by the vapor-liquid separator 10, theliquid alcohol may be, for example, recycled as the heat transfer medium9 to the cooling pipes 7 by means of a pump 11 or can directly beintroduced in the fluidized bed 4 through the line 2 as shown in FIG. 1.

In the present invention, in the above mode of the process shown in FIG.3, a carbon monoxide source together with the liquid alcohol can beintroduced in the cooling pipes 7 as the heat transfer medium 9. Use ofmixture of the alcohol and carbon monoxide decreases the boiling pointof the alcohol and makes it easy not only to vaporize the alcohol butalso to remove the heat of reaction because of the increase of thedifference between the reaction temperature and the boiling point of thealcohol.

The carbon monoxide source introduced together with the liquid alcoholin the cooling pipes 7 is not limited to pure carbon monoxide. A gaseousmixture of carbon monoxide, a gas which is inert in the reaction or aproduct gas withdrawn from the fluidized-bed reactor as mentioned abovecan be used as the carbon monoxide source.

The resultant mixture of the alcohol heated in the cooling pipes 7, andthus at least partially vaporized, and carbon monoxide can be introducedin the above optionally installed vapor-liquid separator 10 by whichliquid alcohol is removed and fed through the line 10a and the line 3into the fluidized bed 4.

For removing the heat of reaction by the above process, it issatisfactory that at least part of the alcohol for use in thecarbonylation is introduced in liquid phase in the cooling pipes 7 asthe heat transfer medium 9. The proportion of the alcohol fed in thecooling pipes 7 generally ranges from about 20 to 100%, preferably, fromabout 70 to 100% based on the total amount of the alcohol used in thecarbonylation.

In the introduction of the alcohol-containing gas produced by thevaporization in the cooling pipes 7 in the fluidized-bed reactor 1, theoperation must be conducted under such conditions that the pressure ofthe alcohol-containing gas at the temperature of the outlet of thecooling pipes 7 is higher than the reaction pressure so as to enable theabove introduction.

In the present invention, still further, the carbonic acid diester canbe produced while vaporizing the alcohol by the heat of reactionaccording to the mode of the process as shown in FIG. 4. That is,cooling pipes 7 are provided in a fluidized bed 4 of a reactor and analcohol as a raw material is introduced in liquid phase thereinto as aheat transfer medium 9 so that the liquid alcohol is heated to have anincreased temperature. Subsequently, the heated liquid alcohol is fedinto an evaporator 12 in which the liquid alcohol is mixed with carbonmonoxide and at least part of the alcohol is vaporized. The vaporizedalcohol can be fed together with the carbon monoxide into thefluidized-bed reactor. Reference characters in FIG. 4 correspond tothose in FIGS. 1 to 3.

Referring to FIG. 4, the evaporator 12 may be provided with an alcoholsupply line 12e and the above alcohol as the heat transfer medium 9 maybe fed from the bottom of the evaporator 12 through a recycle line 12binto the cooling pipes 7 by means of a pump 13. The alcohol supply line12e may be provided at any arbitrary point (not shown) of the recycleline 12b extending from the bottom of the evaporator to the reactorinlet side 7a of the cooling pipes 7.

An alcohol supply line may directly be provided on the reactor inletside 7a of the cooling pipes 7 without providing the recycle line 12bextending from the bottom of the evaporator to the cooling pipes 7.

The alcohol 9 passing through the cooling pipes 7 removes the heat ofreaction from the fluidized bed 4 and, simultaneously, is heated to anincreased temperature. The heated alcohol 9 is introduced through analcohol supply line 14 from a top part 12c of the evaporator into theevaporator 12.

The heated liquid alcohol is mixed with carbon monoxide (the molefraction of the alcohol lowered) in the evaporator 12, so that theboiling point of the alcohol is lowered to thereby cause at least partof the alcohol to vaporize.

Although the type of the evaporator 12 is not limited as long as thevapor and the liquid can satisfactorily contact each other, a packedcolumn and a plate column are preferred. A packed column is especiallypreferred from the viewpoint that the pressure drop is low.

The pressure of the evaporator 12 is preferred to be at least 0.1kg/cm², especially, at least 0.5 kg/cm² higher than the reactionpressure. From the economic point of view, it is preferred that thedifference between the pressure of the evaporator 12 and the reactionpressure is not greater than about 1 kg/cm².

In the evaporator 12, it is preferred that the alcohol is mixed withcarbon monoxide so that a gaseous mixture of carbon monoxide and alcoholwith a molar ratio (CO/alcohol) subjected to the below describedreaction system can be obtained.

Therefore, the temperature of an evaporator outlet 12a is set on thebasis of the calculation from the pressure of the evaporator and thealcohol concentration of the gaseous mixture.

For example, in the synthesis of dimethyl carbonate, when the pressureof the top of the evaporator 12 is 9.2 atm and the alcohol concentrationof the evaporator is 22 mol%, the temperature of the evaporator outlet12a is set at 85° C. which is the dew point of the gaseous mixture.

The temperature of the liquid alcohol as the heat transfer medium 9 at areactor outlet side 7b of the cooling pipes is preferred to have atemperature which is higher than, especially, at least 3° C. higher thanthe temperature of the evaporator outlet 12a.

For example, when the temperature of the evaporator outlet 12a is set at85° C. as mentioned above, the temperature of the alcohol at the reactoroutlet side 7b is preferred to be at least 88° C.

The thus obtained gaseous mixture of vaporized alcohol and carbonmonoxide is discharged from the evaporator outlet 12a and fed through agas supply line 3 into the fluidized-bed reactor 1. This gaseous mixturemay be heated by a heat exchanger 16 as necessary before being fedthrough the gas supply line 3 into the fluidized-bed reactor 1.

The alcohol can be supplied in an amount corresponding to the amount ofalcohol consumed by the carbonylation through the line 12e into theevaporator 12 while controlling the level of the alcohol. On the otherhand, carbon monoxide can be supplied through a line 12f into theevaporator 12. Oxygen can be supplied through the line 3.

In the above modes of the process shown in FIGS. 3 and 4, when thequantity of the heat of reaction is larger than the quantity of heatrequired for the vaporization of the alcohol, the heat removal can beeffected by providing in the fluidized bed 4 a suitable number of othercooling pipes 7 through which, for example, water flows as the heattransfer medium 8 as necessary in addition to the above cooling pipes 7through which the alcohol flows as the heat transfer medium 9.

In the mode of the process shown in FIG. 4, when the quantity of theheat of reaction is larger than the quantity of heat required for thevaporization of the alcohol, alternatively, the heated alcohol supplyline 14 can be provided with an auxiliary heat exchanger 15 so that thealcohol is cooled to an appropriate temperature by, for example, acooling water before being fed into the evaporator 12.

When the quantity of the heat of reaction is smaller than the quantityof heat required for the vaporization of the alcohol, the auxiliary heatexchanger 15 can be used as a heater. In the use as a heater, steam orelectric power can be employed as the heat source.

In the present invention, still further, the carbonic acid diester canbe produced while vaporizing the alcohol by the heat of reactionaccording to the mode of the process as shown in FIG. 5. Referencecharacters in FIG. 5 correspond to those in FIG. 4. This mode of theprocess can be carried out in the following manner.

Cooling pipes 7 are provided as in the above mode and water or an oil asa heat transfer medium 8 is circulated therethrough to thereby obtainhot water or hot oil, this hot water or hot oil 8 being passed through aheat exchanger 19 to thereby effect a heat exchange between the hotwater or oil and a liquid alcohol so that the liquid alcohol is heatedto an increased temperature. This heated liquid alcohol is fed into anevaporator 12 in which the liquid alcohol is mixed with carbon monoxideand at least part of the alcohol is vaporized as in the above mode ofthe process shown in FIG. 4. The vaporized alcohol is fed together withthe carbon monoxide into the fluidized-bed reactor 1.

The heat transfer medium (water or an oil) 8 which flows through thecooling pipes 7 arranged in the fluidized bed 4 removes the heat ofreaction and, simultaneously, is heated. The resultant hot water or hotoil is discharged from the reactor outlet side 7b and led through a heattransfer medium withdrawal line 17 into the heat exchanger 19 in whichthe hot water or hot oil undergoes a heat exchange with the alcohol.

The heat transfer medium 8 cooled by the heat exchanger 19 is recycledto the fluidized-bed reactor 1 as necessary. When the heat transfermedium 8 is recycled, the heat transfer medium 8 cooled by the heatexchanger 19 can first be stored in a heat transfer medium drum 22 and,then, recycled through a line 24 by means of a pump 23 to be introducedin the cooling pipes 7.

The alcohol as a raw material of the carbonylation is heated to anincreased temperature by the heat transfer medium 8 in the heatexchanger 19 and, then, fed through a line 12g to a top part 12c of theevaporator.

In the evaporator 12, as in the mode of the process shown in FIG. 4, theheated liquid alcohol is mixed with carbon monoxide and therebyvaporized. The thus produced gaseous mixture of alcohol and carbonmonoxide is discharged from an evaporator outlet 12a and fed through agas supply line 3 into the fluidized-bed reactor 1.

This gaseous mixture can be heated by means of a heat exchanger 16 asnecessary before being fed through the gas supply line 3 into thefluidized-bed reactor 1.

In the above mode of the process, the alcohol 9 is generally dischargedfrom the bottom of the evaporator 12 and fed through a line 12d into theheat exchanger 19 by means of a pump 21 so that the alcohol 9 is heatedto an increased temperature by the heat exchange with the heat transfermedium 8. The heated alcohol is fed through the line 12g into theevaporator 12.

In the evaporator 12, it is preferred that the alcohol is mixed withcarbon monoxide so that a gaseous mixture of carbon monoxide and alcoholwith a molar ratio which is suitable for the below described reactionsystem can be obtained.

Therefore, the temperature of the evaporator outlet 12a is set on thebasis of the calculation from the pressure of the evaporator and thedesired alcohol concentration of the gaseous mixture.

For example, in the synthesis of dimethyl carbonate, when the pressureof the top of the evaporator 12 is 9.2 atm and the alcohol concentrationof the gaseous mixture is 22 mol%, the temperature of the evaporatoroutlet 12a is set at 85° C. which is the dew point of the gaseousmixture.

Thus, it is requisite that the temperature of the methanol fed throughthe line 12g to the top part 12c of the evaporator is higher than thetemperature of the evaporator outlet 12a (85° C.) and that thetemperature of the heat transfer medium at the reactor outlet side 7b isstill higher than the temperature of the methanol fed to the evaporator.For effective heat exchange, it is desired that the temperature of themethanol at the top part 12c of the evaporator is at least 3° C. higherthan the temperature of the gas of the line 12a and that the temperatureof the heat transfer medium at the reactor outlet side 7b is at least 3°C. higher than the temperature of the methanol at the top part 12c ofthe evaporator.

The alcohol can be supplied in an amount corresponding to the amount ofalcohol consumed by the carbonylation through the line 12e into theevaporator 12 while controlling the level of the alcohol. On the otherhand, carbon monoxide can be supplied through a line 12f into theevaporator 12. Oxygen can be supplied through the line 3. The positionof the alcohol supply line 12e does not necessarily have to be thebottom of the evaporator and can be at any arbitrary point of the line12d extending to the heat exchanger 19. Further, an alcohol supply linemay be directly provided on the heat exchanger 19 without providing therecycle line 12d extending from the bottom of the evaporator to the heatexchanger 19.

When the quantity of the heat of reaction is larger than the quantity ofheat required for the vaporization of the alcohol, it is appropriate todischarge part of the cooling medium outside the system withoutrecycling it or to provide the heat transfer medium withdrawal line 17with an auxiliary heat exchanger 18 so that the alcohol is cooled. Onthe other hand, when the quantity of the heat of reaction is smallerthan the quantity of heat required for the vaporization of the alcohol,it is appropriate to install the auxiliary heat exchanger 18 or a heatexchanger 20 so that the alcohol is heated.

In the present invention, as described above, the alcohol, carbonmonoxide and oxygen react in the vapor phase in the presence of acatalyst while removing the heat of reaction with the direct or indirectutilization of the latent heat of vaporization of the alcohol as a rawmaterial of the carbonylation, thereby obtaining the carbonic aciddiester.

The above alcohol is, for example, an aliphatic alcohol having 1 to 6carbon atoms, an alicyclic alcohol or an aromatic hydroxyl compound.

Examples of suitable alcohols are monohydric alcohols includingsaturated aliphatic alcohols such as methanol, ethanol, propanol,butanol, pentanol and hexanol, unsaturated aliphatic alcohols such asallyl alcohol, alicyclic alcohols such as cyclopropanol, cyclobutanol,cyclopentanol and cyclohexanol, and aromatic hydroxyl compounds such asphenol and benzyl alcohol.

These are used either individually or in combination. Of these, methanoland ethanol are preferred.

In the above reaction system, carbon monoxide is generally used in amolar ratio to alcohol (CO/alcohol) of 0.2 to 100, preferably, 0.5 to 20and, still preferably, 1 to 10. Oxygen is generally used in a molarratio to alcohol (O₂ /alcohol) of 0.01 to 0.5, preferably, 0.05 to 0.3and, still preferably, 0.05 to 0.2.

In the reaction of the above alcohol, carbon monoxide and oxygen, thereaction temperature is generally preferred to range from 70 to 350° C.,especially, from 80 to 250° C., still especially, from 100 to 200° C.and, yet still especially, from 130 to 170° C. The reaction pressure isgenerally preferred to range from atmospheric pressure to 35 kg/cm² G,especially, from 2 to 20 kg/cm² G.

In the present invention, use can be made of a wide variety of solidcatalysts which are commonly employed as catalysts for the oxidativecarbonylation of alcohol. Examples of such solid catalysts for theoxidative carbonylation include those comprising a support such asactive carbon and, carried thereon, a catalytic component such as ametal halide, a mixed metal halide or a metal oxyhalide.

Of suitable metal halides, preferred use is made of a monovalent ordivalent copper halide such as copper chloride or copper bromide.Specific examples of suitable solid catalysts include catalysts having,carried on a support, not only a copper halide, but also (1) an alkalimetal hydroxide and/or an alkaline earth metal hydroxide, e.g., lithiumhydroxide, sodium hydroxide, potassium hydroxide, barium hydroxideand/or calcium hydroxide, (2) (Japanese Patent Publication No.7(1995)-1035, catalysts having, carried on a support, not only a cooperhalide but also a tertiary organophosphorus compound having a phenyl oran alkyl group such as triphenylphosphine, an alkysylarylphosphine, atrialkyl phosphite or a trialkyl phosphate (3) the InternationalApplication Publication WO 90/15791 and catalyst having, carried on asupport, not only a cooper halide but also an inorganic carbonate suchas K₂ CO₃, Na₂ CO₃, CaCO₃, BaCO₃, KNaCO₃, KHCO₃ or (NH₄)₂ CO₃ (4)(Japanese Patent Laid-open Publication No. 7(1995)-194983catalyst.

The above catalysts can be prepared according to the usual methods suchas impregnation, milling and coprecipitation methods commonly employedin causing a catalytic component to be carried on a support.

Examples of the carbonic acid diesters produced by the above modes ofthe process according to the present invention include dimethylcarbonate, diethyl carbonate, dipropyl carbonate, dibutyl carbonate,dipentyl carbonate, dihexyl carbonate, dicyclopropyl carbonate,dicyclobutyl carbonate, dicyclopentyl carbonate, dicyclohexyl carbonate,dibenzyl carbonate, methyl ethyl carbonate, methyl propyl carbonate andethyl propyl carbonate.

Apparatus for producing carbonic acid diester

The present invention provides an apparatus which is suitable for theproduction of a carbonic acid diester according to the above modes ofthe process shown in FIGS. 4 and 5.

One form of the apparatus for producing a carbonic acid diesteraccording to the present invention is shown in FIG. 4.

One form of the apparatus for producing a carbonic acid diesteraccording to the present invention comprises:

a fluidized-bed reactor 1 adapted to carry-out a reaction in a vaporphase of an alcohol, carbon monoxide and oxygen in the presence of acatalyst so that an oxidative carbonylation of the alcohol occurs tothereby form a carbonic acid diester,

an evaporator 12 adapted to mix a liquid alcohol with carbon monoxideand vaporize at least part of the alcohol to thereby form a gaseousmixture of alcohol and carbon monoxide and adapted to feed the gaseousmixture through a gas supply line 3 into the fluidized-bed reactor 1,

cooling pipes 7 arranged in the fluidized-bed reactor 1 and adapted tocause the formation of a liquid alcohol 9 as a heat transfer mediumcapable of removing a heat of reaction generated by the oxidativecarbonylation of the alcohol in the fluidized-bed reactor 1 to flowtherethrough, and

a heated alcohol supply line 14 adapted to feed the liquid alcohol 9heated in the fluidized-bed reactor 1 from the heat cooling pipes 7 intothe evaporator 12.

The above fluidized-bed reactor 1 is provided at a lower part thereofwith a gas distributor la and provided at the top thereof with a productwithdrawal line 5.

Although the type of the evaporator 12 is not particularly limited aslong as it is capable of mixing the liquid alcohol with carbon monoxide.Thus, the evaporator 12 is capable of effecting vaporization of theliquid alcohol, for example, the evaporator can be of the type designedto bring the liquid alcohol and carbon monoxide into a counterflowcontact.

The evaporator 12 is provided with an alcohol supply line 12e and acarbon monoxide supply line 12f. If necessary, a heat exchanger 16 maybe interposed between an evaporator outlet 12a of the evaporator and thesupply line 3.

A line 12b is generally arranged extending from the bottom of theevaporator 12 to the reactor inlet side 7a of the cooling pipes 7 and isprovided with a pump 13 in the middle thereof, so that the alcohol canbe fed to the cooling pipes 7.

The alcohol supply line 12e may be disposed at any arbitrary position ofthe line 12b.

The heated alcohol supply line 14 may be provided with a heat exchanger15.

Moreover, this apparatus may be provided with a vapor-liquid separator 6by which the product gas withdrawn through the line 5 from thefluidized-bed reactor 1 is separated into a gas and a liquid and furtherprovided with a gas recycle line 6a adapted to recycle the gas separatedby the vapor-liquid separator 6 to the evaporator 12. This gas recycleline 6a may be provided with a CO₂ -removing device capable of re-movingby-product carbon dioxide from the gas separated by the vapor-liquidseparator 6 by absorption or adsorption.

This gas recycle line 6a may be provided with a branch pipe 6b capableof discharging the gas outside the reaction system.

Another form of the apparatus for producing a carbonic acid diesteraccording to the present invention is shown in FIG. 5. Referencecharacters in FIG. 5 correspond to those in FIG. 4.

This form of apparatus for producing a carbonic acid diester accordingto the present invention may comprise:

the fluidized-bed reactor 1,

the evaporator 12,

cooling pipes 7 arranged in the fluidized-bed reactor 1 and adapted toform a heat transfer medium 8 capable of removing a heat of reactiongenerated by the oxidative carbonylation of the alcohol in thefluidized-bed reactor 1 to flow therethrough,

a heat transfer medium withdrawal line 17 adapted to lead the heattransfer medium 8 heated in the fluidized-bed reactor 1 from the coolingpipes 7 to a heat exchanger 19,

the heat exchanger 19 adapted to conduct a heat exchange between theheat transfer medium 8 and liquid alcohol 9 so that the liquid alcohol 9is heated to an increased temperature, and

a heated alcohol supply line 12g adapted to feed the liquid alcohol 9heated by the heat exchanger 19 into the evaporator 12.

In this form of the apparatus, it is generally preferred that water oran oil is used as the heat transfer medium 8.

The heat transfer medium withdrawal line 17 may be provided with anauxiliary heat exchanger 18. Further, the apparatus may be provided witha line 24 through which the heat transfer medium 8 cooled by the heatexchange with the alcohol by means of the heat exchanger 19 is recycledto the cooling pipes 7 by means of a pump 23. This line 24 may beprovided with a heat transfer medium drum 22 in which the heat transfermedium 8 having undergone the heat exchange is temporarily stocked.

The heated alcohol supply line 12g may be provided with an auxiliaryheat exchanger 20. A line 12d extending from the bottom of theevaporator to the heat exchanger 19 is generally provided with a pump21.

Moreover, this apparatus may be provided with a vapor-liquid separator 6by which the product gas withdrawn through the line 5 from thefluidized-bed reactor 1 is separated into a gas and a liquid and furtherprovided with a gas recycle line 6a adapted to recycle the gas separatedby the vapor-liquid separator 6 to the evaporator 12. This gas recycleline 6a may be provided with a CO₂ -removing device capable of removingby-product carbon dioxide from the gas separated by the vapor-liquidseparator 6 by absorption or adsorption.

This gas recycle line 6a may be provided with a branch pipe 6b capableof discharging the gas outside the reaction system.

EFFECT OF THE INVENTION

The present invention provides a process for producing a carbonic aciddiester in a vapor phase with the use of a fluidized-bed reactor, bywhich the carbonic acid diester can be produced in high energyefficiency by effective utilization of the heat of reaction.

Further, the present invention provides an apparatus for producing acarbonic acid diester which is suitable for use in carrying out theabove process.

EXAMPLE

The present invention will now be illustrated in greater detail withreference to the following Examples, which in no way limit the scope ofthe invention.

In the following Examples and Comparative Examples, use was made of thecatalyst prepared by causing active carbon to carry copper (II) chlorideand sodium hydroxide in a molar ratio of OH/Cu of 1.2 and at a coppercontent of 6% by weight.

Preparation of catalyst

37 kg of copper (II) chloride dehydrate was dissolved in distilled waterto obtain 100 lit. of an aqueous copper chloride solution (a).

13 kg of sodium hydroxide was dissolved in distilled water to obtain 100lit. of an aqueous sodium hydroxide solution (b).

100 kg of active carbon was impregnated with 50 lit. of the aboveaqueous copper chloride solution (a), dried at 130° C. for 3 hr flowingnitrogen gas and cooled. The resultant copper chloride carrying activecarbon was impregnated with 40 lit. of the above aqueous sodiumhydroxide solution (b) and dried at 130° C. for 3 hr flowing nitrogengas, thereby obtaining a catalyst for use in a fluidized bed.

This catalyst had a copper content of 6% by weight and a molar ratio ofOH/Cu of 1.2. The Cu content was calculated by the formula: ##EQU1##

Example 1

Six U-shaped cooling pipes each having an outside diameter of 34 mm anda length of straight line part of 1 m were inserted in a fluidized-bedreactor of 350 mm in diameter having a height of catalyst-packed bed of1500 mm. The U-shaped cooling pipes were arranged so as to allowrespective cooling mediums different from each other to flowtherethrough.

Nitrogen heated at 140° C. was fed at a flow rate of 112 kg/h into thefluidized-bed reactor through a gas distributor disposed at a bottom ofthe fluidized-bed reactor, and the pressure in the fluidized-bed reactorwas controlled at 9 atm.

Subsequently, methanol which was heated to 140° C. and thereby vaporizedwas fed at a rate of 10 kg/h into the fluidized-bed reactor, and,further, CO and O₂ were fed with the feeding rate of nitrogen reduced sothat the feeding rates of CO and O₂ were finally 112 kg/h and 9.6 kg/h,respectively, and the feeding of N₂ was discontinued.

Thereafter, a liquid methanol heated to 80° C. was directly fed justabove the gas distributor into the fluidized bed at a rate of 5 kg/h.The feeding rate of the liquid methanol was gradually increased whilethe feeding rate of the vaporized methanol was gradually decreased untilall the methanol became fed in liquid phase at a rate of 64 kg/h.

Under this condition, the reaction was continued for 6 hr. Throughoutthe reaction, cooling by passing 80 ° C. water through only three of theU-shaped cooling pipes enabled desirably controlling the reactiontemperature at 140 ±3° C.

The composition analysis and the flow rate measurement of the reactoreffluent gas showed that the methanol conversion was 31% and thedi-methyl carbonate (DMC) selectivity was 90%. The DMC yield determinedfrom the material balance was 25 kg/h.

Comparative Example 1

The same fluidized-bed reactor as in Example 1 was used and the reactionpressure was controlled at 9 atm by nitrogen in the same manner as inExample 1.

Subsequently, methanol which was heated to 140° C. and therebyvaporized, CO and O₂ were fed into the fluidized-bed reactor atrespective rates of 10, 112 and 9.6 kg/h, and the feeding of nitrogenwas discontinued. 80° C. water was initially passed through only threeof the cooling pipes, and, while gradually increasing the feeding rateof vaporized methanol, the number of cooling pipes through which hotwater was passed was increased. However, when the feeding rate ofvaporized methanol was increased to 50 kg/h, the reaction temperaturecontinued to increase irrespective of the feeding of hot water to all ofthe six cooling pipes with the result that the CO₂ concentration of theeffluent gas exhibited a grave increase.

Therefore, the feeding rate of vaporized methanol was decreased to 42kg/h and the operation was continued for 6 hr. The reaction temperaturecould be controlled at 145 ±5° C.

The methanol conversion, DMC selectivity and DMC yield were 29%, 89% and15 kg/h, respectively.

It was found that the DMC yield of Example 1 was 1.7 times that ofComparative Example 1 and that the utility corresponding to 70% of thecooling duty and all the heat of vaporization of methanol could be savedin Example 1 as compared with those of Comparative Example 1.

Example 2

The same fluidized-bed reactor as in Example 1 was used and the reactionpressure was controlled at 4 atm by nitrogen in the same manner as inExample 1.

Subsequently, methanol which was heated to 140° C. and thereby vaporizedwas fed at a rate of 5 kg/h into the fluidized-bed reactor, and,further, CO and O₂ were fed with the feeding rate of nitrogen reduced sothat the feeding rates of CO and O₂ were finally 52 kg/h and 4.5 kg/h,respectively, and the feeding of N₂ was discontinued.

Thereafter, a liquid methanol heated to 80° C. was directly fed justabove the gas distributor into the fluidized bed at a rate of 5 kg/h.The feeding rate of the liquid methanol was gradually increased whilethe feeding rate of the vaporized methanol was gradually decreased untilall the methanol became fed in liquid phase at a rate of 30 kg/h.

80° C. water was passed through only one of the U-shaped cooling pipes,and the reaction was continued for 5 hr.

The composition analysis and the flow rate measurement of the reactoreffluent gas showed that the methanol conversion was 30% and thedimethyl carbonate (DMC) selectivity was 91%. The DMC yield determinedfrom the material balance was 11 kg/h.

Example 3

The same fluidized-bed reactor as in Example 1 was used and the reactionpressure was controlled at 4 atm by nitrogen in the same manner as inExample 1.

Subsequently, methanol which was heated to 140° C. and thereby vaporizedwas fed at a rate of 5 kg/h into the fluidized-bed reactor, and,further, CO and O₂ were fed with the feeding rate of nitrogen reduced sothat the feeding rates of CO and O₂ were finally 52 kg/h and 4.5 kg/h,respectively, and the feeding of N₂ was discontinued.

Thereafter, a liquid methanol was fed to four of the U-shaped coolingpipes, vaporized at pressure of 4.2 atm and fed into the fluidized bedreactor at a rate of 5 kg/h. Of the methanol fed into the fluidized-bedreactor, the feeding rate of the methanol vaporized in the cooling pipeswas gradually increased while the feeding rate of the methanol vaporizedoutside the reactor was decreased until only the methanol vaporized inthe cooling pipes became fed at a rate of 30 kg/h.

The reaction was continued for 5 hr under this condition while passing80° C. water through another two of the cooling pipes.

The methanol conversion, DMC selectivity and DMC yield were 30%, 90% and11 kg/h, respectively.

Example 4

The same fluidized-bed reactor as in Example 1 was used and the reactionpressure was controlled at 4 atm by nitrogen in the same manner as inExample 1.

Subsequently, methanol which was heated to 140° C. and thereby vaporizedwas fed at a rate of 5 kg/h into the fluidized-bed reactor, and,further, CO and O₂ were fed with the feeding rate of nitrogen reduced sothat the feeding rates of CO and O₂ were finally 52 kg/h and 4.5 kg/h,respectively, and the feeding of N₂ was discontinued.

Thereafter, CO and a liquid methanol were mixed together and fed tothree of the U-shaped cooling pipes, causing the methanol to vaporize atan intra-pipe temperature controlled at 95° C., and fed into thefluidized bed reactor. The feeding rates of the methanol and CO at theinitial feeding points were decreased until the methanol and CO finallyfed into the fluidized-bed reactor entirely through the cooling pipes.The vaporized methanol and CO were fed at respective rates of 30 kg/hand 52 kg/h.

The reaction was continued for 5 hr under this condition while passing80° C. water through another two of the cooling pipes.

The methanol conversion, DMC selectivity and DMC yield were 30%, 91% and11 kg/h, respectively.

Comparative Example 2

The same fluidized-bed reactor as in Example 1 was used and the reactionpressure was controlled at 4 atm by nitrogen in the same manner as inExample 1.

Subsequently, methanol which was heated to 140° C. and therebyvaporized, CO and O₂ were fed into the fluidized-bed reactor atrespective rates of 10, 52 and 4.5 kg/h, and the feeding of nitrogen wasdiscontinued. 80° C. water was initially passed through only one of theU-shaped cooling pipes, and, while gradually increasing the feeding rateof vaporized methanol, the number of cooling pipes through which hotwater was passed was increased. Finally, the reaction temperature couldbe controlled at 145±50° C. by increasing the feeding rate of vaporizedmethanol to 30 kg/h and by feeding hot water to five of the coolingpipes.

The methanol conversion, DMC selectivity and DMC yield were 28%, 89% and10 kg/h, respectively.

It was found that the utility corresponding to 76% of the cooling dutyand all the heat of vaporization of methanol could be saved in Examples2 to 4 as compared with those of Comparative Example 2.

Example 5

The same fluidized-bed reactor as in Example 1 was used and the reactionpressure was controlled at 9 atm by nitrogen in the same manner as inExample 1.

Nitrogen heated to 140° C. was fed at a flow rate of 112 kg/h into thefluidized-bed reactor through a gas distributor disposed at a bottom ofthe fluidized-bed reactor, and the pressure of the fluidized-bed reactorwas controlled at 9 atm.

Subsequently, ethanol which was heated to 155° C. and thereby vaporizedwas fed at a rate of 10 kg/h into the fluidized-bed reactor, and,further, CO and O₂ were fed with the feeding rate of nitrogen reduced sothat the feeding rates of CO and O₂ were finally 112 kg/h and 9.6 kg/h,respectively, and the feeding of N₂ was discontinued.

Thereafter, a liquid ethanol heated to 80° C. was directly fed justabove the gas distributor into the fluidized bed at a rate of 5 kg/h.The feeding rate of the liquid ethanol was gradually increased while thefeeding rate of the vaporized ethanol was gradually decreased until allthe ethanol became fed in liquid phase at a rate of 92 kg/h.

Under this condition, the reaction was continued for 6 hr. Throughoutthe reaction, cooling by passing 80° C. water through only two of theU-shaped cooling pipes enabled the desirable control of the reactiontemperature at 140±3° C.

The composition analysis and the flow rate measurement of the reactoreffluent gas showed that the ethanol conversion was 27% and the diethylcarbonate (DEC) selectivity was 87%. The DEC yield determined from thematerial balance was 28 kg/h.

Comparative Example 3

The same fluidized-bed reactor as in Example 1 was used and the reactionpressure was controlled at 9 atm by nitrogen in the same manner as inExample 1.

Subsequently, ethanol which was heated to 155° C. and thereby vaporized,CO and O₂ were fed into the fluidized-bed reactor at respective rates of10, 112 and 9.6 kg/h, and the feeding of nitrogen was discontinued. 80°C. water was initially passed through only two of the U-shaped coolingpipes, and, while gradually increasing the feeding rate of vaporizedethanol, the number of cooling pipes through which hot water was passedwas increased. However, when the feeding rate of vaporized ethanol wasincreased to 60 kg/h, the reaction temperature continued to increaseirrespective of the feeding of hot water to all the six cooling pipeswith the result that the CO₂ concentration of the effluent gas exhibiteda grave increase.

Therefore, the feeding rate of vaporized ethanol was decreased to 57kg/h and the operation was continued for 6 hr.

The ethanol conversion, DEC selectivity and DEC yield were 26%, 87% and17 kg/h, respectively.

It was found that the DEC yield of Example 5 was 1.6 times that ofComparative Example 3 and that the utility corresponding to 85% of thecooling duty and all the heat of vaporization of ethanol could be savedin Example 5 as compared with those of Comparative Example 3.

Example 6

Dimethyl carbonate was produced by the use of the apparatus shown inFIG. 4, which was not provided, however, with the gas recycle line 6a.

Six U-shaped cooling pipes each having an outside diameter of 34 mm anda length of straight line part of 1 m were inserted in a fluidized-bedreactor of 350 mm in diameter having a height of catalyst-packed bed of1500 mm. Methanol was introduced in all the U-shaped cooling pipes.

Nitrogen heated to 140° C. was fed at a flow rate of 100 kg/h into thefluidized-bed reactor through a gas distributor disposed at a bottom ofthe fluidized-bed reactor, and the pressure of the fluidized-bed reactorwas controlled at 9 atm. Subsequently, methanol which was heated to 140°C. and thereby vaporized was fed at a rate of 10 kg/h into thefluidized-bed reactor, and, further, CO containing 10 mol% of hydrogenand O₂ were fed with the feeding rate of nitrogen reduced so that,finally, the feeding rates of CO containing 10 mcl% of hydrogen and O₂were 144 kg/h and 8.2 kg/h, respectively, with the feeding of nitrogendiscontinued.

Thereafter, pressurized liquid methanol was fed at a flow rate of 1200kg/h to the cooling pipes. The methanol from the outlets of the coolingpipes was cooled to 90° C. by a heat exchanger 15 and fed to an upperpart of an alcohol evaporator. The liquid methanol was withdrawn fromthe bottom thereof and recycled to the cooling pipes. The CO flow pathwhich had supplied the fluidized-bed reactor with CO was switched so asto feed CO to the bottom of the alcohol evaporator, and the outlet gasof the alcohol evaporator was heated to 120° C. and fed into thefluidized-bed reactor.

Further, methanol was fed to the bottom of the alcohol evaporator whilecontrolling the level of the liquid surface.

In the steady state, the alcohol supply and the temperature of the topof the evaporator were 54 kg/h and 85° C., respectively, and the coolingpipe inlet temperature, cooling pipe outlet temperature and supplytemperature to evaporator of the methanol were 67° C., 101° C. and 90°C., respectively.

The composition analysis and the flow rate measurement of the reactoreffluent gas showed that the methanol conversion was 30% and the DMCselectivity was 91%. The DMC yield determined from the material balancewas 21 kg/h. The reaction temperature could appropriately be controlledat 145±2° C.

The utility corresponding to 68% of the cooling duty and all the heat ofvaporization of methanol during the steady-state operation could besaved in Example 6.

Example 7

Dimethyl carbonate was produced by the use of the apparatus shown inFIG. 5, which was not provided, however, with the gas recycle line 6a.

Six U-shaped cooling pipes each having an outside diameter of 34 mm anda length of straight line part of 1 m were inserted in a fluidized-bedreactor of 350 mm in diameter having a height of catalyst-packed bed of1500 mm. Water was introduced in all the U-shaped cooling pipes.

Nitrogen heated to 140° C. was fed at a flow rate of 100 kg/h into thefluidized-bed reactor through a gas distributor disposed at a bottom ofthe fluidized-bed reactor, and the pressure of the fluidized-bed reactorwas controlled at 9 atm. Subsequently, methanol which was heated to 140°C. and thereby vaporized was fed at a rate of 10 kg/h into thefluidized-bed reactor, and, further, CO containing 15 mol% of CO₂ and O₂were fed with the feeding rate of N₂ reduced so that, finally, thefeeding rates of CO containing 15 mol% of CO₂ and O₂ were 166 kg/h and7.4 kg/h, respectively, with the feeding of N₂ discontinued.

Thereafter, methanol was recycled from the bottom of the alcoholevaporator to the top thereof at a flow rate of 1200 kg/h.Simultaneously, 79° C. water was fed at a flow rate of 1000 kg/h to thecooling pipes, and the hot water from the outlet thereof was cooled to95° C. by means of a heat exchanger 18. The hot water was fed to a heatexchanger 19 attached to the alcohol evaporator in which the methanolwas heated by the hot water. The CO flow path which had supplied thefluidized-bed reactor with CO was switched so as to feed CO to thebottom of the alcohol evaporator, and the outlet of the alcoholevaporator was heated to 120° C. and fed into the fluidized-bed reactor.

Further, methanol was fed to the bottom of the alcohol evaporator whilecontrolling the level of the liquid surface.

In the steady state, the alcohol supply, the temperature of theevaporator top, the temperature of the evaporator bottom, the coolingpipe inlet temperature and the cooling pipe outlet temperature were 50kg/h, 85° C., 68° C., 79° C. and 102° C., respectively.

The composition analysis and the flow rate measurement of the reactoreffluent gas showed that the methanol conversion was 30% and the DMCselectivity was 90%. The DMC yield determined from the material balancewas 19 kg/h.

The reaction temperature could appropriately be controlled at 145±2° C.

The utility corresponding to 69% of the cooling duty and all the heat ofvaporization of methanol during the steady-state operation could besaved in Example 7.

What is claimed is:
 1. An apparatus for producing a carbonic acid diester, which comprises:a fluidized-bed reactor (1) adapted to carry out a reaction in a vapor phase of an alcohol, carbon monoxide and oxygen in the presence of a catalyst so that an oxidative carbonylation of the alcohol occurs to hereby form a carbonic acid diester, an evaporator (12) adapted to mix a liquid alcohol with carbon monoxide and vaporize at least part of the alcohol to thereby form a gaseous mixture of alcohol and carbon monoxide and adapted to feed the gaseous mixture through a gas supply line (3) into the fluidized-bed reactor (1), cooling pipes (7) arranged in the fluidized-bed reactor (1) and adapted to cause a liquid alcohol (9) as a raw material as a heat transfer medium capable of removing a heat of reaction generated by the oxidative carbonylation of the alcohol in the fluidized-bed reactor (1) to flow therethrough, and a heated alcohol supply line (14) adapted to feed the liquid alcohol (9) heated in the fluidized-bed reactor (1) from the cooling pipes (7) into the evaporator (12).
 2. An apparatus for producing a carbonic acid diester, which comprises:a fluidized-bed reactor (1) adapted to carry out a reaction in a vapor phase of an alcohol, carbon monoxide and oxygen in the presence of a catalyst so that an oxidative carbonylation of the alcohol occurs to thereby form a carbonic acid diester, an evaporator (12) adapted to mix a liquid alcohol with carbon monoxide and vaporize at least part of the alcohol to thereby form a gaseous mixture of alcohol and carbon monoxide and adapted to feed the gaseous mixture through a gas supply line (3) into the fluidized-bed reactor (1), cooling pipes (7) arranged in the fluidized-bed reactor (1) and adapted to cause a heat transfer medium (8) capable of removing a heat of reaction generated by the oxidative carbonylation of the alcohol in the fluidized-bed reactor (1) to flow therethrough, a heat transfer medium withdrawal line (17) adapted to lead the heat transfer medium (8) heated in the fluidized-bed reactor (1) from the cooling pipes (7) to a heat exchanger(19), the heat exchanger (19) adapted to conduct a heat exchange between the heat transfer medium (8) and a liquid alcohol (9) as a raw material so that the liquid alcohol (9) is heated to an increased temperature, and a heated alcohol supply line (12g) adapted to feed the liquid alcohol (9) heated by the heat exchanger (19) into the evaporator (12). 